EP1833593A1 - Device for purifying a gas stream containing condensable vapours - Google Patents

Device for purifying a gas stream containing condensable vapours

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Publication number
EP1833593A1
EP1833593A1 EP05825747A EP05825747A EP1833593A1 EP 1833593 A1 EP1833593 A1 EP 1833593A1 EP 05825747 A EP05825747 A EP 05825747A EP 05825747 A EP05825747 A EP 05825747A EP 1833593 A1 EP1833593 A1 EP 1833593A1
Authority
EP
European Patent Office
Prior art keywords
separation
ferrule
filtration
gas
electrode
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP05825747A
Other languages
German (de)
French (fr)
Other versions
EP1833593B1 (en
Inventor
Méryl BROTHIER
Jean-Pierre Turchet
Pierre Estubier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Commissariat a lEnergie Atomique et aux Energies Alternatives CEA
Original Assignee
Commissariat a lEnergie Atomique CEA
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Commissariat a lEnergie Atomique CEA filed Critical Commissariat a lEnergie Atomique CEA
Priority to PL05825747T priority Critical patent/PL1833593T3/en
Publication of EP1833593A1 publication Critical patent/EP1833593A1/en
Application granted granted Critical
Publication of EP1833593B1 publication Critical patent/EP1833593B1/en
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D8/00—Cold traps; Cold baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
    • B03C3/01—Pretreatment of the gases prior to electrostatic precipitation
    • B03C3/014—Addition of water; Heat exchange, e.g. by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
    • B03C3/02—Plant or installations having external electricity supply
    • B03C3/04—Plant or installations having external electricity supply dry type
    • B03C3/06—Plant or installations having external electricity supply dry type characterised by presence of stationary tube electrodes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
    • B03C3/02—Plant or installations having external electricity supply
    • B03C3/04—Plant or installations having external electricity supply dry type
    • B03C3/14—Plant or installations having external electricity supply dry type characterised by the additional use of mechanical effects, e.g. gravity
    • B03C3/15—Centrifugal forces

Definitions

  • the invention relates to a device for separating condensable vapors from a gas stream loaded with fines or not. More particularly, it relates to a device for maintaining the composition of the incondensable gas stream and the recovery of condensates for their subsequent use or simply their separate treatment.
  • This media can be both liquid (of the solvent type injected by nebulization within the separator) and solid (of the fiber or membrane type) that can constitute the separation medium (see the separative approach by absorption-adsorption).
  • This option of using a sparge to purify the gas can prove to be relatively effective even if it generates effluents in greater or lesser amounts with a concomitant risk of driving on the one hand of the splash liquid and therefore of pollution of the gas to be treated.
  • US Patent 4,723,970 relates to a gas / water separation device based on a centrifugal separation. This device is compact but does not allow a thorough separation.
  • DE 8 905 182 relates to a vapor-liquid separation system with combined filtration.
  • WO 9 208 937 relates to an assembly for extracting condensable species from a gaseous flow by centrifugation coupled with cooling. It only ensures a limited level of purification insofar as no separation medium is used.
  • US 3,890,122 relates to a multi-stage filtration apparatus involving separation by centrifugation, condensation and filtration on filter media. This device however has a number of disadvantages:
  • the centrifugal separation is mainly ensured by a helical calender body imposing a separation efficiency according to the flow rate or the operating pressure
  • the invention therefore aims to provide a device for purifying a gas flow that overcomes these disadvantages. It should be compact in view of gas flow rates that it can process, insensitive to the presence of fines in the stream to be purified, and able to operate continuously or at least minimizing the frequency of slagging the device. he Moreover, it will have to be flexible in its mode of operation to enable its conduct to be adapted to the desired separation conditions, for example able to generate a flow of condensates free of additives in the case where the condensates constitute the noble material to be recovered.
  • the device for purifying a gas stream containing condensable vapors comprises a shell defining a sealed volume, a cooler for quenching the gas stream, a rotating assembly comprising a rotor and a cylindrical shell of separation and filtration mounted on the rotor and rotating with it, a support tube mounted on the rotor and carrying a device turbulator-scraper, an electrode surrounding the separation ferrule and filtration and a central counter-electrode for the creation of an electrostatic field in the grille, a purified gas outlet pipe, a condensate outlet pipe ensuring the evacuation while ensuring the tightness of the system.
  • the separating and filtering ferrule consists of superimposed crenellated circular rings, at least one impact and separation plate being fixed on each of the rings of the ferrule.
  • the separation and filtration sleeve consists of thermally insulating rings and thermally conductive impaction plates making it possible to ensure a controlled thermal transfer between the zone inside the separation-filtration ferrule and a thermostated zone.
  • the separation and filtration ferrule is made of absorbent materials capable of capturing the condensable species.
  • the thermostated zone surrounds the separation and filtration ferrule.
  • the purified gas outlet pipe can simultaneously act as a counter-electrode.
  • FIG. 1 is a block diagram of a theoretical number of stages fixed by the process characteristics of the device
  • FIG. 2 is a block diagram showing the flows and major functions of a purification device according to the invention.
  • FIG. 3 is a sectional view of an embodiment of a purification device according to the present invention.
  • FIG. 4 is a partial sectional view along the line IV-IV of Figure 3;
  • FIG. 5 is a detailed view of the separation and filtration media of the device of FIG. 3;
  • FIG. 6 is a sectional view according to the reference VI-VI of Figure 5;
  • FIG. 8 is a sectional view of a cryocondenser for use in a purification device according to the invention.
  • FIG. 9 is a schematic sectional view of a plate separator used as a reference.
  • Figure 1 a conventional block diagram in chemical engineering which represents in a simplified manner a theoretical number of stages fixed by the process characteristics of the device.
  • the latter comprises a finite number of stages, 2,4, ... n, as shown schematically by the dashed line lines 6.
  • These stages are housed in a shell 7.
  • the line between mixed X schematizes the axis of rotation of the device.
  • the vertical axis indicates an increasing degree of purification of the gas and the horizontal axis H the distance to the axis of symmetry X of the device.
  • the gas to be purified shown schematically by the arrow 10 enters the first stage 2.
  • a condensing medium 12 is introduced at this level.
  • Part of the condensable vapors containing particles maintained in a solid-liquid equilibrium (condensed state) is extracted from the gas to be purified as shown schematically by the arrow 14.
  • the accumulated condensed phase In contact with the impact plates, the accumulated condensed phase is partially liquefied and can thus traverse (mark 55) the media 54 while limiting the entrainment of the gas phase of the thermostated zone.
  • the liquid is then extracted from the device as shown schematically by the arrow 20.
  • the gas to be purified then passes to the second stage, designated by the reference 4, as shown schematically by the arrow 22. And so on.
  • the purified gas leaves the apparatus at the top as represented by the arrow 30.
  • FIG. 2 is a block diagram showing on the flow plane and functions / elements, the subsystems corresponding to the major functions of the device of the invention.
  • a heat exchanger 32 for example a cryocondenser cooled with liquid nitrogen.
  • the gas to be purified designated by reference 10
  • a condensing medium designated by the reference 12.
  • This condensation medium also called additive, is chosen according to its physicochemical properties which must be taken into account to obtain the best nucleation possible.
  • the gas stream 10 may optionally be pre-cooled prior to quenching it in the heat exchanger 32, for example by circulating through a heat pipe 34. This cooling step allows an additional degree of freedom with respect to the quenching possibility in the heat exchanger 32.
  • the heat pipe 34 is considered as not making part of the device defined by the shell 7 schematized by the dashed lines in Figure 2.
  • FIG. 3 shows an exemplary embodiment of a purification device according to the invention. It comprises a base 39 and a lower flange 41 fixed relative to the base 39. A shell 7 is mounted on the lower flange 41 and carries at its upper part an upper flange 52.
  • a rotating assembly 42 is mounted on the base 39 and on the flange 41 via a bearing 43 ball bearing.
  • the rotating assembly 42 comprises an axis 44 on which is mounted a circular plate 46 and a perforated tube 48. It is rotated, for example by means of an electric motor not shown.
  • the perforated tube 48 carries three comb scrapers 50 arranged at 120 ° from each other (see Figure 4). Condensates in the non-gaseous sense of the term
  • a cylindrical separation and filtration ring 54 is mounted on the plate 46 and rotates at the same time as this plate.
  • the shell 54 consists of rings 56 superimposed.
  • the rings 56 comprise crenellations 60 which delimit between them perforated portions 62.
  • Impact plates are fixed externally to each of the rings 56.
  • the plates 64 are fixed for example by means of screws 66.
  • Each plate 64 has a portion 68 , preferably inclined towards the inside of the shell 54? which is located opposite the recesses 62 and which constitutes the impact plate proper.
  • the shell 54 can be easily dismantled and cleaned.
  • a holding flange 70 ensures the maintenance of all the rings.
  • the flange 70 is rotatably mounted with the rotor. It turns relative at a fixed bearing 72 with which a rotating sealing level, more or less important can be achieved.
  • this design allows to combine the necessary insulation between the cold zones and thermostated and maintaining a heat transfer to allow the condensate to migrate to the thermostated portion.
  • the tube 48 comprises two longitudinal slots 49 whose function is to allow the evacuation of the gas stream via the tube 78.
  • a heat exchanger 36 is mounted under the upper flange 52. It has the shape of a cylindrical shell which surrounds the perforated tube 48 to which it is arranged coaxially.
  • the combs 50 rotate in the space defined by the exchanger 36. A slight clearance is provided between the end of the combs and the inner wall of the exchanger 36.
  • the tube 78 is mounted coaxially with the axis X of the device.
  • the lower end of the tube 78 is housed inside the perforated tube 48.
  • the upper part of the rod 78 passes through the upper flange 52.
  • the rod 78 allows the output of the treated gas.
  • the inlet of the gas to be treated is, in turn, through a tube 80 which passes through the upper flange 52.
  • the tube 80 opens into the volume defined by the inner wall of the cylindrical exchanger 36, that is to say in the volume swept by the combs 50.
  • Pipes 82 and 84 respectively allow the supply and discharge of a cryogenic fluid, for example liquid nitrogen, into the exchanger 36.
  • a heating element 86 may surround the shell 7.
  • all or part of the stream treated (or even that to be treated) discharged by the rod 78 may be recirculated in the annular volume defined between the periphery of the shell 54 and the shell 7 by the pipe 88 so as to constitute a thermostated zone 18.
  • An auxiliary fluid may also be injected through a pipe 90.
  • the orifice 90 serves to introduce the condensing media corresponding to the reference number 12 (see FIG. 2) and thus to promote nucleation. It allows the precipitation of a condensate mist.
  • This additive nebulized upstream of the quench, and chosen for its physicochemical properties (condensation temperature, polarity, miscibility, permittivity) adapted to the purification case that we are trying to achieve, especially if it is either to recover the condensate is primarily to purify the flow entering the system.
  • a cylindrical electrode 94 is disposed outside the ferrule 54.
  • the electrode 94 may be disposed within the shell 7, as shown in Figure 3, or externally to this shell.
  • the evacuation rod of the treated gas stream 78 acts as a counter electrode.
  • a generally fixed potential difference is established between the electrode 94 and the counter electrode 78 so as to promote electrostatic precipitation.
  • the condensation medium will preferably be chosen so as to to promote this precipitation (joint consideration between the diameter of particles formed by the condensation of the mixture) media-auxiliary (channel 90) / condensate and the permeativity of these particles.
  • Rotating assembly 42 allows the flow to be centrifuged at speeds that are sufficient for a separation rate of the condensate particles adapted to the desired purification case.
  • This step makes it possible to migrate the particles to the filter medium, in this case the filtering and separating ring 54, at a speed that is sufficient relative to their residence time in the purification device.
  • the filter medium in this case the filtering and separating ring 54
  • the time required for a particle to settle can therefore be expressed as follows:
  • N rotation frequency a: radius of rotation
  • Rcanne radius of the exit rod of the gases to be purified (non-free zone)
  • D diameter of the particles
  • ⁇ viscosity of the gas to be purified
  • ⁇ p difference in density between the condensate particle and the gas to be treated.
  • Centrifugation is optionally promoted by the combined action of an electrostatic field generated within the separation zone, as previously explained.
  • the speed Uc of migration (or collection) of the condensate particles by the electrostatic effect alone can be expressed by a relation of the type:
  • the filtering medium 54 makes it possible to constitute an impaction barrier favoring the recondensation of the contensate particles and the enrichment in condensates on the side of the shell 7.
  • the constituent elements of the media advantageously consist of thermally insulating elements and then conductive elements. thermally in the radial direction from the inner zone of the filter media 54 to its outer face (facing the thermostated zone 18); this to ensure a temperature maintenance both on the centrifugal side (the inside of the shell 54) that the side of the shell 7 to promote the transfer of the condensate and its flow before it is discharged by the purge systems in continuous 40.
  • the objective is to form aggregates of solid / liquid particles 69 on the inner faces of the impingement plates 68 (FIGS. 5 and 6).
  • the slight temperature gradient controlled and imposed by the thermostated zone 18 then allows liquefaction and the formation of a condensate film 98 (FIG. 7) that can be evacuated by the clearances 69 arranged between the impaction and temperature distribution elements 68 and the media (the shroud 54) also serves as a thermal barrier.
  • a liquid jet of 71 strikes the shell 7 and a film of liquid 73 is deposited on this one.
  • the passages 69 also make it possible to control the pressure drop at the level of the media and to compensate for its clogging, particularly in the case where the latter consists of absorption-adsorption capture elements.
  • the performance of the device of the invention is based on the combined effects of centrifugation, impaction, cooling, electrostatic field, nucleation and finally adsorption. Nevertheless, beyond the combination of these separative approaches and the adaptability of the process, the originality of the present invention lies in the separation / purification method combining a phase change and a combined separation. To achieve this result and to minimize both the entrainment of gas in condensates or vice versa, condensates in the gas stream, a film of solid material consisting of condensable materials (mixed or not with a condensing media if objective is to recover the condensables or rather to enhance the gas flow) is itself an interphase guaranteeing the separation of flows.
  • the heat flux imposed on the area outside the filtration media makes it possible to maintain an equilibrium and a temperature gradient between the solid film and the impact and thermal distribution plates.
  • the condensables migrate outside the inlet zone of the gas charged with condensables towards the thermostated zone while forming a film that avoids driving the charged gas.
  • the design of the apparatus also makes it possible to play on the thickness of the film (for example by applying a suitable temperature in the thermostated zone) to obtain more or less important separative performance levels depending on the nature of the condensables.
  • the filter media zone in the case where it is made of absorbent materials capable of capturing the condensable species.
  • the adjustment for example by adjusting the rotational speed of the device or by choosing a type of specific absorption media) between the absorption force and the centripetal force makes it possible to control the clogging rate of the media and hence the quantity condensable species migrating to the collection area.
  • FIG. 8 shows a sectional view of another embodiment of a cryocondensor that can be used in the context of a gas flow purification device according to the invention. It comprises a tube bundle 100 (only two tubes have been shown in FIG. 8) inside a cylindrical shell 102 itself. The tubes 100 are secured at their upper ends with a flange 105, and at their lower ends, with a flange 106.
  • a ferrule 108 made for example of stainless steel, is mounted under the flange 106.
  • the gas to be purified is introduced into the bundle of the tubes 100, as shown schematically by the arrows 112. It opens into the interior volume defined by the shell 108.
  • a cryogenic liquid for example liquid nitrogen, circulates around the tubes 100 so as to perform a quenching of the gas to be purified.
  • FIG. 9 shows a plate separator used as a reference in order to compare its performance with that of a constituent device and in accordance with the invention (cryocondensor).
  • This apparatus of simple constitution has a cone 120 at its upper part. This cone is connected to an outer cylinder 122 on the inner wall of which are disposed a series of conical shaped plates 124.
  • An inner tube 126 is disposed in the tube 122 coaxially with the latter.
  • the inner tube 126 also carries plates 128 conical or frustoconical.
  • the inner tube 122 and the outer tube 126 are cooled to a temperature of -5 0 C to -1O 0 C by a circulation of a coolant generally glycol water.
  • the entry of the brine into the outer tube has been represented by the arrow 130 and its exit by the arrow 132.
  • the arrows 134 and 136 schematize respectively the introduction and the evacuation of the brine in the inner tube. 126.
  • the stream to be purified is introduced at the top of the cone as shown by the arrow 140. It follows a sinuous course defined by the frustoconical elements 124 and 128 before leaving the apparatus at its lower part as shown by the arrow 142.
  • the flow of gas to be treated (pyrolysis gas of biomass produced around 500 0 C) still has enough condensates to disturb the measurement. flow rate given by a flow meter Coriolis type.
  • the condensate content in the stream changes from 100 g / Nm 3 to 10 g / Nm 3 (see FIG. 10).
  • the passage times of the gases to be treated are of the order of ten seconds.
  • two plate separators in series for example of the type shown in FIG. 9, have been used to obtain the above-mentioned level of purification.
  • a cryocondensing device such as that represented in FIG. 8 was used and implanted complementarily following the two plate separators.
  • the additional purification tests with this device made it possible to observe the possibility of forming condensate particles of variable diameters exceeding rarely 0.5 mm depending on the humidity. present in the gas to be purified.
  • the residence times in this device are close to the second.
  • FIG. 14 The result of this treatment is shown in FIG. 14.
  • the curves of FIGS. 10, 11 and 12 give order-of-magnitude numerical elements of the local overpressure parameters at the separation media and the performances that can be expected for particle diameters (vesicle and / or solid) and given rotational speeds.
  • Figure 10 gives the relationship between the local pressure and the wall pressure (P (r) / P (a)) as a function of the dimension (r / a).
  • Figure 11 gives the sedimentation time as a function of the particle diameter (inertial effect alone) and
  • Figure 12 the maximum gas flow rate to reach the sedimentation time of the particles.
  • Figure 13 shows the flow measured by coriolis effect with a plate separator and Figure 14 with cryocondenser and filter media.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Electrostatic Separation (AREA)
  • Treating Waste Gases (AREA)
  • Separating Particles In Gases By Inertia (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

A purifier comprises a cylinder (7) with a sealed inner volume, a cooler (36) for tempering the gas flow, a rotary assembly (42) with a rotor (44) and a separation/filtration ring (54), a supporting tube (48) for a turbulence generator and scraper, an electrode (94) surrounding the ring and a central counter-electrode (78) for creating an electrostatic field inside the cylinder. It also has an outlet tube for the purified gases and a channel (40) that ensures full evacuation of condensates. The separation/filtration ring comprises a number of superimposed toothed rings with an impact/separation plate attached to each, or from thermal insulating rings and thermal conducting plates to ensure a controlled heat transfer between the interior of the ring a thermostatic zone (18).

Description

DISPOSITIF D'EPtJRATION D'UN FLUX GAZEUX CONTENANT DES DEVICE FOR EPTIMATING A GAS STREAM CONTAINING
VAPEURS CONDENSABLESCONDENSABLE VAPORS
DESCRIPTIONDESCRIPTION
DOMAINE TECHNIQUETECHNICAL AREA
L'invention concerne un dispositif de séparation de vapeurs condensables d'un flux gazeux chargé en fines ou non. Plus particulièrement, elle concerne un dispositif permettant un maintien de la composition du flux gazeux incondensable et la récupération des condensats pour leur emploi ultérieur ou simplement leur traitement séparé.The invention relates to a device for separating condensable vapors from a gas stream loaded with fines or not. More particularly, it relates to a device for maintaining the composition of the incondensable gas stream and the recovery of condensates for their subsequent use or simply their separate treatment.
ETAT DE LA TECHNIQUE ANTERIEURESTATE OF THE PRIOR ART
De nombreux procédés de type physico¬ chimique (thermolyse, méthanisation...) génèrent des gaz potentiellement valorisables . Toutefois ils doivent préalablement subir une épuration pour être compatibles avec les critères de qualité permettant leur utilisation dans d'autres procédés (co-génération, synthèse de carburants...) . La problématique de traitement de ces gaz est donc un point clé dans ce processus de valorisation. De nombreuses solutions techniques ont été mises au point pour résoudre ce problème. Elles peuvent être classées dans six grandes familles : Approche thermique : ce type de technique constitue la solution radicale dans la mesure où il est admissible de porter à haute température le gaz valorisable. On entend par admissible le fait qu'il existe une possibilité de chauffer le gaz sans qu'il y ait perte de la qualité de ce dernier. Par contre cette approche n'est pas toujours admissible (au-delà de toute considération économique) , comme par exemple en cas de présence simultanée de carburant et de comburant. Par ailleurs, ce type de traitement ne permet pas de récupérer les espèces séparées (parce qu'il entraîne généralement leur destruction partielle ou totale) ce qui peut constituer un handicap rédhibitoire pour le cas où ces espèces (hormis le gaz valorisable) présentent elles-mêmes un potentiel de valorisation. Enfin, des considérations de rendement énergétique rendent souvent cette approche peu rentable. Approche oxydante : dans ce cas l'énergie apportée aux gaz à épurer l'est sous forme de potentiel chimique, généralement par le biais d'un oxydant qui est communément l'oxygène pur ou bien celui constitutif de l'air. Dans cette configuration, au contraire de l'approche purement thermique qui consiste uniquement à porter en température le gaz à traiter, le traitement est souvent moins consommateur d'énergie puisque l' exothermicité des réactions d'oxydation est exploitée. Néanmoins, la contre-partie de cette approche est non seulement une destruction des espèces condensables, ce qui est un inconvénient dans le cas où elles seraient valorisables, mais aussi une modification de la qualité des gaz à épurer liée à une dilution par le produit d' oxydation des espèces pouvant l'être dans les conditions du traitement. Approche séparative par changement d'état : cette approche repose sur la différence de la température de changement d'état des espèces constitutives du gaz à épurer, et notamment sur leur température de condensation. Des températures plus ou moins basses peuvent être nécessaires, ce qui peut conduire à des dispositifs de purification relativement lourds à mettre en œuvre. Par ailleurs, la séparation obtenue n'est généralement pas totale du fait de limitations physiques (considérations liées aux tensions de vapeur, notamment) . Pour améliorer la séparation, il est alors possible d'utiliser un média favorisant le captage de l'espèce à séparer. Ce média peut être aussi bien liquide (de type solvant injecté par nébulisation au sein du séparateur) que solide (de type fibre ou membrane) pouvant constituer le média de séparation (voir l'approche séparative par absorption- adsorption) . L'option d'utiliser un barbotage pour épurer le gaz peut s'avérer quant à elle relativement efficace même si elle génère des effluents en quantités plus ou moins importantes avec un risque concomitant d'entraînement d'une part du liquide de barbotage et donc de pollution du gaz à traiter.Many physical ¬ chemical type processes (thermolysis, methanisation ...) generate potentially recoverable gas. However, they must first be purified to be compatible with the quality criteria for their use in other processes (co-generation, fuel synthesis ...). The problem of treating these gases is therefore a key point in this valuation process. Many technical solutions have been developed to solve this problem. They can be classified in six main families: Thermal approach: this type of technique is the radical solution insofar as it is acceptable to bring the high-value gas to high temperature. Qualifying means the fact that There is a possibility to heat the gas without losing the quality of the gas. On the other hand, this approach is not always admissible (beyond any economic consideration), for example in the case of the simultaneous presence of fuel and oxidizer. Moreover, this type of treatment does not make it possible to recover the separated species (because it usually leads to their partial or total destruction) which can constitute a crippling handicap in the event that these species (apart from the valorizable gas) present themselves. same potential valuation. Finally, energy efficiency considerations often make this approach uneconomic. Oxidizing approach: in this case the energy supplied to the gases to be purified is in the form of chemical potential, generally through an oxidant which is commonly pure oxygen or the constituent of air. In this configuration, unlike the purely thermal approach which consists only in bringing the gas to be treated to temperature, the treatment is often less energy consuming since the exothermicity of the oxidation reactions is exploited. Nevertheless, the counterpart of this approach is not only a destruction of the condensable species, which is a disadvantage in the case where they would be recoverable, but also a modification of the quality of the gases to be purified linked to a dilution by the product of oxidation of species that can be in the conditions of treatment. Separative approach by change of state: this approach is based on the difference of the change of state temperature of the constituent species of the gas to be purified, and in particular on their condensation temperature. More or less low temperatures may be necessary, which may lead to relatively heavy purification devices to implement. Moreover, the separation obtained is generally not total because of physical limitations (considerations related to vapor pressures, in particular). To improve the separation, it is then possible to use a media promoting the capture of the species to be separated. This media can be both liquid (of the solvent type injected by nebulization within the separator) and solid (of the fiber or membrane type) that can constitute the separation medium (see the separative approach by absorption-adsorption). The option of using a sparge to purify the gas can prove to be relatively effective even if it generates effluents in greater or lesser amounts with a concomitant risk of driving on the one hand of the splash liquid and therefore of pollution of the gas to be treated.
Approche séparative par effet mécanique : cette approche repose sur différents effets :Separative approach by mechanical effect: this approach is based on different effects:
• L'effet centrifuge appliqué sur des espèces constitutives du gaz à épurer et ayant des masses différentes. Le cas de la séparation isotopique peut même être traité par ce type d' approche (ultra- centrifugation) même si elle présente l'inconvénient d'être relativement onéreuse. • L'effet d' impaction favorisant l'agglomé¬ ration de fines particules de condensats augmentant par là même l'effet de centrifugation.• The centrifugal effect applied to constituent species of the gas to be purified and having different masses. The case of isotopic separation can even be treated by this type of approach (ultracentrifugation) even if it has the disadvantage of being relatively expensive. • The impaction effect favoring the agglomeration ¬ ration of fine condensate particles thereby increasing the centrifugation effect.
• La filtration via un média spécifique et/ou le dépôt de filtration (gâteau) pouvant lui-même faire office de média constitué in situ, phénomène améliorant la filtration.• The filtration via a specific media and / or the filtration deposit (cake) can itself act as media formed in situ, improving filtration phenomenon.
Approche séparative par affinité de charge électrique (effet de polarité) , phénomène notamment exploité dans les électro-précipitateurs de filtration des gaz .Separative approach by affinity of electric charge (effect of polarity), phenomenon notably exploited in electro-precipitators of gas filtration.
Approche séparative par absorption- adsorption, phénomène d'autant plus efficace qu'il se produit à basse température. Ces différentes approches présentent des inconvénients génériques (dégradation de la qualité des produits, rendement, coût...) mais aussi des limitations propres à chaque application pour en décliner l'application industrielle. C'est pourquoi de nouvelles approches combinant un certain nombre des approches précipitées ont été mises au point :Separative approach by absorption-adsorption, a phenomenon which is all the more effective when it occurs at low temperatures. These different approaches have generic disadvantages (degradation of product quality, yield, cost ...) but also limitations specific to each application to decline industrial application. This is why new approaches combining a number of hasty approaches have been developed:
Le brevet US 4 723 970 concerne un dispositif de séparation gaz/eau s' appuyant sur une séparation centrifuge. Ce dispositif est compact mais ne permet pas une séparation poussée.US Patent 4,723,970 relates to a gas / water separation device based on a centrifugal separation. This device is compact but does not allow a thorough separation.
Le brevet DE 8 905 182 concerne un système de séparation liquide vapeur avec filtration combinée.DE 8 905 182 relates to a vapor-liquid separation system with combined filtration.
Cet ensemble ne présente notamment aucune fonction de condensation poussée ce qui limite son application à l'épuration de vapeur constitutive d'un flux gazeux sale ou non. Le document WO 9 208 937 concerne un ensemble d'extraction d'espèces condensables d'un flux gazeux par centrifugation couplé à un refroidissement. Il ne permet d'assurer qu'un niveau d'épuration limité dans la mesure notamment où aucun média de séparation n'est mis en œuvre.This assembly does not have any particular function of extensive condensation which limits its application to the purification of steam constituting a dirty gas stream or not. WO 9 208 937 relates to an assembly for extracting condensable species from a gaseous flow by centrifugation coupled with cooling. It only ensures a limited level of purification insofar as no separation medium is used.
Le document US 3 890 122 concerne un appareil de filtration multi-étagé faisant intervenir la séparation par centrifugation, condensation et filtration sur média filtrant. Ce dispositif présente toutefois un certain nombre d'inconvénients :US 3,890,122 relates to a multi-stage filtration apparatus involving separation by centrifugation, condensation and filtration on filter media. This device however has a number of disadvantages:
II est dédié au traitement de l'air comprimé. Il est conçu pour une épuration spécifique et limitée notamment en ce qui concerne la présence éventuelle de vapeurs condensables plus ou moins volatiles .It is dedicated to the treatment of compressed air. It is designed for a specific and limited purification especially with regard to the possible presence of condensable vapors more or less volatile.
La séparation par centrifugation est principalement assurée par un corps de calandre hélicoïdale imposant une efficacité de séparation en fonction du débit ou de la pression de fonctionnementThe centrifugal separation is mainly ensured by a helical calender body imposing a separation efficiency according to the flow rate or the operating pressure
(couplage du dispositif à un compresseur) . Le dispositif souffre ainsi d'un manque de degrés de liberté concernant son mode de pilotage. Enfin, il n'est pas compact. L'invention a par conséquent pour objet de proposer un dispositif d'épuration d'un flux gazeux qui remédie à ces inconvénients. Il devra être compact au vu des débits de flux gazeux qu'il peut traiter, peu sensible à la présence de fines dans le flux à épurer, et capable de fonctionner en continu ou du moins en minimisant la fréquence de décrassage du dispositif. Il devra en outre être flexible par son mode de fonctionnement pour permettre d' adapter sa conduite aux conditions de séparation recherchées, par exemple apte à générer un flux de condensats exempts d'additifs dans le cas où les condensats constituent la matière noble à récupérer. D'une manière générale, il devra ainsi tout aussi bien s'adapter à l'épuration du flux gazeux à proprement parler (cas où le flux à valoriser est le gaz) qu'à la récupération des espèces condensables (cas où les vapeurs condensables constituent la matière à valoriser) .(coupling the device to a compressor). The device thus suffers from a lack of degrees of freedom concerning its driving mode. Finally, it is not compact. The invention therefore aims to provide a device for purifying a gas flow that overcomes these disadvantages. It should be compact in view of gas flow rates that it can process, insensitive to the presence of fines in the stream to be purified, and able to operate continuously or at least minimizing the frequency of slagging the device. he Moreover, it will have to be flexible in its mode of operation to enable its conduct to be adapted to the desired separation conditions, for example able to generate a flow of condensates free of additives in the case where the condensates constitute the noble material to be recovered. In a general way, it will thus have to adapt equally to the purification of the gas flow strictly speaking (in which the flux to be valorized is the gas) than to the recovery of the condensable species (case where the condensable vapors constitute the material to be valued).
Ces buts sont atteints par le fait que le dispositif d'épuration d'un flux gazeux contenant des vapeurs condensables, comprend une calandre définissant un volume étanche, un refroidisseur pour tremper le flux gazeux, un ensemble tournant comprenant un rotor et une virole cylindrique de séparation et filtration montée sur le rotor et tournant avec lui, un tube support monté sur le rotor et portant un dispositif turbuleur-racleur, une électrode entourant la virole de séparation et filtration et une contre-électrode centrale pour la création d'un champ électrostatique dans la calandre, une canalisation de sortie du gaz épuré, une canne de sortie des condensats assurant l'évacuation tout en garantissant l'étanchéité du système.These objects are achieved by the fact that the device for purifying a gas stream containing condensable vapors comprises a shell defining a sealed volume, a cooler for quenching the gas stream, a rotating assembly comprising a rotor and a cylindrical shell of separation and filtration mounted on the rotor and rotating with it, a support tube mounted on the rotor and carrying a device turbulator-scraper, an electrode surrounding the separation ferrule and filtration and a central counter-electrode for the creation of an electrostatic field in the grille, a purified gas outlet pipe, a condensate outlet pipe ensuring the evacuation while ensuring the tightness of the system.
De préférence la virole de séparation et filtration est constituée d' anneaux circulaires crénelés superposés, au moins une plaque d'impact et de séparation étant fixée sur chacun des anneaux de la virole. Avantageusement, la virole de séparation et filtration est constituée d' anneaux thermiquement isolants et de plaques d' impaction thermiquement conductrices permettant d'assurer un transfert thermique maîtrisé entre la zone interne à la virole de séparation-filtration et une zone thermostatée.Preferably, the separating and filtering ferrule consists of superimposed crenellated circular rings, at least one impact and separation plate being fixed on each of the rings of the ferrule. Advantageously, the separation and filtration sleeve consists of thermally insulating rings and thermally conductive impaction plates making it possible to ensure a controlled thermal transfer between the zone inside the separation-filtration ferrule and a thermostated zone.
Avantageusement encore la virole de séparation et filtration est constituée de matériaux absorbants aptes à capter les espèces condensables . Dans une réalisation, la zone thermostatée entoure la virole de séparation et filtration.Advantageously, the separation and filtration ferrule is made of absorbent materials capable of capturing the condensable species. In one embodiment, the thermostated zone surrounds the separation and filtration ferrule.
La canalisation de sortie du gaz épuré peut jouer simultanément le rôle de contre-électrode.The purified gas outlet pipe can simultaneously act as a counter-electrode.
BRÈVE DESCRIPTION DES DESSINSBRIEF DESCRIPTION OF THE DRAWINGS
D'autres caractéristiques et avantages de l'invention apparaîtront encore à la lecture de la description qui suit d'exemples de réalisation donnés en référence aux figures annexées. Sur ces figures : - la figure 1 est un schéma de principe d'un nombre d'étages théorique fixé par les caractéristiques procédé du dispositif ;Other features and advantages of the invention will become apparent on reading the following description of embodiments given with reference to the appended figures. In these figures: - Figure 1 is a block diagram of a theoretical number of stages fixed by the process characteristics of the device;
- la figure 2 est un schéma de principe représentant les flux et les grandes fonctions d'un dispositif d'épuration conforme à l'invention ;FIG. 2 is a block diagram showing the flows and major functions of a purification device according to the invention;
- la figure 3 est une vue en coupe d'un mode de réalisation d'un dispositif d'épuration conforme à la présente invention ;FIG. 3 is a sectional view of an embodiment of a purification device according to the present invention;
- la figure 4 est une vue en coupe partielle selon la ligne IV-IV de la figure 3 ; - la figure 5 est une vue de détail du média de séparation et de filtration du dispositif de la figure 3 ;- Figure 4 is a partial sectional view along the line IV-IV of Figure 3; FIG. 5 is a detailed view of the separation and filtration media of the device of FIG. 3;
- la figure 6 est une vue en coupe selon le repère VI-VI de la figure 5 ;- Figure 6 is a sectional view according to the reference VI-VI of Figure 5;
- la figure 7 illustre le principe de séparation et de transfert des condensats ;- Figure 7 illustrates the principle of separation and transfer of condensate;
- la figure 8 est une vue en coupe d'un cryocondenseur destiné à être utilisé dans un dispositif d'épuration conforme à l'invention ;- Figure 8 is a sectional view of a cryocondenser for use in a purification device according to the invention;
- la figure 9 est une vue schématique en coupe d'un dévésiculeur à plaques utilisé en référence ;- Figure 9 is a schematic sectional view of a plate separator used as a reference;
- les figures 10 à 14 sont des courbes comparatives qui mettent en évidence les avantages d'un dispositif selon l'invention.- Figures 10 to 14 are comparative curves which highlight the advantages of a device according to the invention.
On a représenté sur la figure 1 un schéma de principe classique en génie chimique qui représente de manière simplifiée un nombre d'étage théorique fixé par les caractéristiques procédé du dispositif. Ce dernier comporte un nombre fini d'étages, 2,4,...n, comme schématisé par les lignes en trait pointillé 6. Ces étages sont logés dans une calandre 7.There is shown in Figure 1 a conventional block diagram in chemical engineering which represents in a simplified manner a theoretical number of stages fixed by the process characteristics of the device. The latter comprises a finite number of stages, 2,4, ... n, as shown schematically by the dashed line lines 6. These stages are housed in a shell 7.
La ligne entre mixte X schématise l'axe de rotation du dispositif. L'axe vertical indique un degré de purification croissante du gaz et l'axe horizontal H la distance à l'axe de symétrie X du dispositif. Le gaz à épurer, schématisé par la flèche 10 pénètre dans le premier étage 2. Un média de condensation 12 est introduit à ce niveau. Une partie des vapeurs condensables contenant des particules maintenues dans un équilibre solide-liquide (état condensé) est extrait du gaz à épurer comme schématisé par la flèche 14. Au contact des plaques d'impact, la phase condensée accumulée est partiellement liquéfiée et peut ainsi traverser (repère 55) le média 54 tout en limitant l'entraînement de la phase gazeuse de la zone thermostatée. Le liquide est alors extrait du dispositif comme schématisé par la flèche 20. Le gaz à épurer passe ensuite au second étage, désigné par la référence 4, comme schématisé par la flèche 22. Et ainsi de suite. Le gaz épuré sort de l'appareil à la partie supérieure comme représenté par la flèche 30.The line between mixed X schematizes the axis of rotation of the device. The vertical axis indicates an increasing degree of purification of the gas and the horizontal axis H the distance to the axis of symmetry X of the device. The gas to be purified, shown schematically by the arrow 10 enters the first stage 2. A condensing medium 12 is introduced at this level. Part of the condensable vapors containing particles maintained in a solid-liquid equilibrium (condensed state) is extracted from the gas to be purified as shown schematically by the arrow 14. In contact with the impact plates, the accumulated condensed phase is partially liquefied and can thus traverse (mark 55) the media 54 while limiting the entrainment of the gas phase of the thermostated zone. The liquid is then extracted from the device as shown schematically by the arrow 20. The gas to be purified then passes to the second stage, designated by the reference 4, as shown schematically by the arrow 22. And so on. The purified gas leaves the apparatus at the top as represented by the arrow 30.
La figure 2 est un schéma de principe représentant sur le plan flux et fonctions/éléments, les sous systèmes correspondants aux grandes fonctions du dispositif de l'invention. Dans la calandre 7 déjà mentionnée, on trouve un échangeur de chaleur 32, par exemple un cryocondenseur refroidi à l'azote liquide. Le gaz à épurer, désigné par référence 10, est mélangé à un média de condensation désigné par la référence 12. Ce média de condensation, également appelé additif, est choisi en fonction de ses propriétés physico-chimiques qui sont à prendre en compte pour obtenir la meilleure nucléation possible. Le flux gazeux 10 peut optionnellement être pré-refroidi préalablement à sa trempe dans l' échangeur de chaleur 32, par exemple par une circulation à travers un caloduc 34. Cette étape de refroidissement permet un degré de liberté supplémentaire par rapport à la possibilité de trempe dans l' échangeur 32. En ce sens le caloduc 34 est considéré comme ne faisant pas partie du dispositif délimité par la calandre 7 schématisée par les traits tiretés sur la figure 2.FIG. 2 is a block diagram showing on the flow plane and functions / elements, the subsystems corresponding to the major functions of the device of the invention. In the calender 7 already mentioned, there is a heat exchanger 32, for example a cryocondenser cooled with liquid nitrogen. The gas to be purified, designated by reference 10, is mixed with a condensing medium designated by the reference 12. This condensation medium, also called additive, is chosen according to its physicochemical properties which must be taken into account to obtain the best nucleation possible. The gas stream 10 may optionally be pre-cooled prior to quenching it in the heat exchanger 32, for example by circulating through a heat pipe 34. This cooling step allows an additional degree of freedom with respect to the quenching possibility in the heat exchanger 32. In this sense, the heat pipe 34 is considered as not making part of the device defined by the shell 7 schematized by the dashed lines in Figure 2.
La fonction de centrifugation est symbolisée par le losange 36. Le flux gazeux traverse ensuite un média de filtration 54 disposé concentriquement par rapport à l'axe de symétrie de rotation X du dispositif. Les condensats sont évacués à la partie inférieure de l'appareil par une pompe ou un siphon 40 permettant de maintenir l'étanchéité du système. Le gaz épuré sort en 37. Il peut être recirculé dans la zone thermostatée 18 (flèche 35) avant de sortir de cette zone (flèche 37) . Le flux gazeux à traiter 10 peut également être utilisé pour thermostater la zone 18 le cas échéant. On a représenté sur la figure 3 un exemple de réalisation d'un dispositif d'épuration conforme à l'invention. Il comporte un socle 39 et une bride inférieure 41 fixe par rapport au socle 39. Une calandre 7 est montée sur la bride inférieure 41 est elle porte à sa partie supérieure une bride supérieure 52.The centrifugation function is symbolized by the rhombus 36. The gas stream then passes through a filtration medium 54 arranged concentrically with respect to the axis of rotation symmetry X of the device. The condensates are evacuated at the bottom of the unit by a pump or siphon 40 to maintain the tightness of the system. The purified gas leaves at 37. It can be recirculated in the thermostated zone 18 (arrow 35) before exiting this zone (arrow 37). The gas stream to be treated may also be used to thermostate zone 18 if necessary. FIG. 3 shows an exemplary embodiment of a purification device according to the invention. It comprises a base 39 and a lower flange 41 fixed relative to the base 39. A shell 7 is mounted on the lower flange 41 and carries at its upper part an upper flange 52.
Un ensemble tournant 42 est monté sur le socle 39 et sur la bride 41 par l'intermédiaire d'un palier 43 à roulement à billes. L'ensemble tournant 42 comprend un axe 44 sur lequel est monté un plateau circulaire 46 et un tube ajouré 48. Il est entraîné en rotation, par exemple au moyen d'un moteur électrique non représenté. A son extrémité supérieure, le tube ajouré 48 porte trois peignes racleurs 50 disposés à 120° l'un de l'autre (voir figure 4) . Les condensats au sens non gazeux du termeA rotating assembly 42 is mounted on the base 39 and on the flange 41 via a bearing 43 ball bearing. The rotating assembly 42 comprises an axis 44 on which is mounted a circular plate 46 and a perforated tube 48. It is rotated, for example by means of an electric motor not shown. At its upper end, the perforated tube 48 carries three comb scrapers 50 arranged at 120 ° from each other (see Figure 4). Condensates in the non-gaseous sense of the term
(c'est-à-dire liquides ou solides) ont naturellement tendance à se déposer et à s'agglomérer dans certains angles de l'appareil, en particulier sur les points froids et fixes, en l'occurrence la paroi périphérique intérieure de l'échangeur 36. Il est donc indispensable, afin de garantir la fonction de refroidissement, d'empêcher Ces dépôts qui dégradent fortement le coefficient d' échange thermique de l'échangeur. Les peignes racleurs ont précisément pour fonction de les empêcher en brassant le flux gazeux dans le volume intérieur de l'échangeur 36.(ie liquid or solid) have a natural tendency to settle and to agglomerate in certain angles of the apparatus, in particular on the cold and fixed points, in this case the inner peripheral wall of the Exchanger 36. It is therefore essential, in order to guarantee the cooling function, to prevent these deposits which strongly degrade the heat exchange coefficient of the heat exchanger. The scraping combs have the precise function of preventing them by stirring the gas flow in the interior volume of the exchanger 36.
Une virole cylindrique de séparation et de filtration 54 est montée sur le plateau 46 et tourne en même temps que ce plateau. Comme on peut le voir plus particulièrement sur les figures 5 et 6, la virole 54 est constituée d'anneaux 56 superposés. Les anneaux 56 comportent des créneaux 60 qui délimitent entre eux des parties ajourées 62. Des plaques d'impact sont fixées extérieurement à chacun des anneaux 56. Les plaques 64 sont fixées par exemple au moyen de vis 66. Chaque plaque 64 comporte une partie 68, de préférence inclinée vers l'intérieur de la virole 54? qui est située en regard des évidements 62 et qui constitue la plaque d'impact proprement dite.A cylindrical separation and filtration ring 54 is mounted on the plate 46 and rotates at the same time as this plate. As can be seen more particularly in Figures 5 and 6, the shell 54 consists of rings 56 superimposed. The rings 56 comprise crenellations 60 which delimit between them perforated portions 62. Impact plates are fixed externally to each of the rings 56. The plates 64 are fixed for example by means of screws 66. Each plate 64 has a portion 68 , preferably inclined towards the inside of the shell 54? which is located opposite the recesses 62 and which constitutes the impact plate proper.
Grâce à cette réalisation sous forme d'anneaux, la virole 54 peut être facilement démontée et nettoyée. Une bride de maintien 70 assure le maintien de l'ensemble des anneaux. La bride 70 est montée tournante avec le rotor. Elle tourne par rapport à un palier fixe 72 avec lequel un niveau d'étanchéité tournante, plus ou moins importante peut être réalisé.Thanks to this embodiment in the form of rings, the shell 54 can be easily dismantled and cleaned. A holding flange 70 ensures the maintenance of all the rings. The flange 70 is rotatably mounted with the rotor. It turns relative at a fixed bearing 72 with which a rotating sealing level, more or less important can be achieved.
Par ailleurs, cette conception permet d'allier l'isolation nécessaire entre les zones froides et thermostatée et le maintien d'un transfert de chaleur pour permettre au condensât de migrer vers la partie thermostatée.Furthermore, this design allows to combine the necessary insulation between the cold zones and thermostated and maintaining a heat transfer to allow the condensate to migrate to the thermostated portion.
Comme on peut le voir également sur la figure 4, le tube 48 comporte deux lumières longitudinales 49 qui ont pour fonction de permettre l'évacuation du flux gazeux via le tube 78.As can also be seen in FIG. 4, the tube 48 comprises two longitudinal slots 49 whose function is to allow the evacuation of the gas stream via the tube 78.
Un échangeur de chaleur 36 est monté sous la bride supérieure 52. Il présente la forme d'une virole cylindrique qui entoure le tube ajouré 48 auquel il est disposé coaxialement . Les peignes 50 tournent dans l'espace délimité par l' échangeur 36. Un léger jeu est prévu entre l'extrémité des peignes et la paroi intérieure de l' échangeur 36.A heat exchanger 36 is mounted under the upper flange 52. It has the shape of a cylindrical shell which surrounds the perforated tube 48 to which it is arranged coaxially. The combs 50 rotate in the space defined by the exchanger 36. A slight clearance is provided between the end of the combs and the inner wall of the exchanger 36.
Le tube 78 est monté coaxialement à l'axe X du dispositif. L'extrémité inférieure du tube 78 est logée à l'intérieur du tube ajouré 48. La partie supérieure du la canne 78 traverse la bride supérieure 52. La canne 78 permet la sortie du gaz traité. L'entrée du gaz à traiter se fait, quant à elle, par un tube 80 qui traverse la bride supérieure 52. Le tube 80 débouche dans le volume défini par la paroi interne de 1' échangeur cylindrique 36, c'est-à-dire dans le volume balayé par les peignes 50. Des canalisations 82 et 84 permettent respectivement l'amenée et l'évacuation d'un fluide cryogénique, par exemple l'azote liquide, dans 1' échangeur 36. Optionnellement un élément chauffant 86 peut entourer la calandre 7. En outre, la totalité ou une partie du flux traité (voire celui à traiter) évacué par la canne 78 peut être recirculé dans le volume annulaire définit entre la périphérie de la virole 54 et la calandre 7 par la canalisation 88 de manière à constituer une zone thermostatée 18.The tube 78 is mounted coaxially with the axis X of the device. The lower end of the tube 78 is housed inside the perforated tube 48. The upper part of the rod 78 passes through the upper flange 52. The rod 78 allows the output of the treated gas. The inlet of the gas to be treated is, in turn, through a tube 80 which passes through the upper flange 52. The tube 80 opens into the volume defined by the inner wall of the cylindrical exchanger 36, that is to say in the volume swept by the combs 50. Pipes 82 and 84 respectively allow the supply and discharge of a cryogenic fluid, for example liquid nitrogen, into the exchanger 36. Optionally, a heating element 86 may surround the shell 7. In addition, all or part of the stream treated (or even that to be treated) discharged by the rod 78 may be recirculated in the annular volume defined between the periphery of the shell 54 and the shell 7 by the pipe 88 so as to constitute a thermostated zone 18.
Un fluide auxiliaire peut en outre être injecté par une tubulure 90. L'orifice 90 a pour fonction l'introduction du média de condensation correspondant au numéro de référence 12 (voir figure 2) et donc de favoriser la nucléation. Il permet la précipitation d'un brouillard de condensât. Cet additif nébulisé en amont de la trempe, et choisi pour ses propriétés physico-chimiques (température de condensation, polarité, miscibilité, permittivité) adaptées au cas d'épuration que l'on cherche à atteindre, notamment s'il s'agit soit de récupérer le condensât soit prioritairement d'épurer le flux entrant dans le système.An auxiliary fluid may also be injected through a pipe 90. The orifice 90 serves to introduce the condensing media corresponding to the reference number 12 (see FIG. 2) and thus to promote nucleation. It allows the precipitation of a condensate mist. This additive nebulized upstream of the quench, and chosen for its physicochemical properties (condensation temperature, polarity, miscibility, permittivity) adapted to the purification case that we are trying to achieve, especially if it is either to recover the condensate is primarily to purify the flow entering the system.
Dans une réalisation préférée, une électrode cylindrique 94 est disposée à l'extérieur de la virole 54. L'électrode 94 peut être disposée à l'intérieur de la calandre 7, comme représenté sur la figure 3, ou extérieurement à cette calandre. Avantageusement, la canne d'évacuation du flux gazeux traité 78 joue le rôle de contre électrode. On établit une différence de potentiel, généralement fixe, entre l'électrode 94 et la contre électrode 78 de manière à favoriser une précipitation électrostatique. Le média de condensation sera de préférence choisi de manière à favoriser cette précipitation (considération conjuguée entre le diamètre de particules formées par la condensation du mélange) média-auxiliaire (canalisation 90) /condensât et la permétivité de ces particules. L'ensemble tournant 42 permet une centrifugation du flux à des vitesses suffisantes pour un taux de séparation des particules de condensât adapté au cas d'épuration souhaité. Cette étape permet de faire migrer les particules vers le média filtrant, en l'occurrence la virole 54 de filtration et de séparation, à une vitesse suffisante par rapport à leur temps de séjour dans le dispositif d'épuration. Pour la conception de la zone de centrifugation, il est possible en première approximation de déterminer la vitesse limite de migration d'une particule en supposant l'égalité des forces centrifuge et de Stockes telle qu'il est possible de l'évaluer pour des particules dont le diamètre moyen équivalent est compris approximativement entre 1 et 50μm. Le temps nécessaire à une particule pour sédimenter peut donc être exprimé comme suit :In a preferred embodiment, a cylindrical electrode 94 is disposed outside the ferrule 54. The electrode 94 may be disposed within the shell 7, as shown in Figure 3, or externally to this shell. Advantageously, the evacuation rod of the treated gas stream 78 acts as a counter electrode. A generally fixed potential difference is established between the electrode 94 and the counter electrode 78 so as to promote electrostatic precipitation. The condensation medium will preferably be chosen so as to to promote this precipitation (joint consideration between the diameter of particles formed by the condensation of the mixture) media-auxiliary (channel 90) / condensate and the permeativity of these particles. Rotating assembly 42 allows the flow to be centrifuged at speeds that are sufficient for a separation rate of the condensate particles adapted to the desired purification case. This step makes it possible to migrate the particles to the filter medium, in this case the filtering and separating ring 54, at a speed that is sufficient relative to their residence time in the purification device. For the design of the centrifugation zone, it is possible, as a first approximation, to determine the limit speed of migration of a particle by assuming the equality of the centrifugal forces and of the stocks as it is possible to evaluate it for particles. whose average equivalent diameter is approximately between 1 and 50 .mu.m. The time required for a particle to settle can therefore be expressed as follows:
τ. log(aIRcanné) τjr 9η τ . log (aIRcanned) τjr 9η
U =Kc.-^ ; - (1) avec Kc= 'U = Kc. - (1) with Kc = '
(ND)2 2π2Ap(ND) 2 2π 2 Ap
et :and
N : fréquence de rotation a : rayon de rotationN: rotation frequency a: radius of rotation
Rcanne : rayon de la canne de sortie des gaz à épurer (zone non libre) D : diamètre des particules η : viscosité du gaz à épurer Δp : différence de masse volumique entre la particule de condensât et le gaz à traiter.Rcanne: radius of the exit rod of the gases to be purified (non-free zone) D: diameter of the particles η: viscosity of the gas to be purified Δp: difference in density between the condensate particle and the gas to be treated.
En s' appuyant sur la relation (1), il est possible pour un dimensionnement et une vitesse de rotation donnés de représenter le temps de sédimentation des particules en fonction de leur diamètre moyen. On a ainsi l'expression d'une droite en échelle logarithmique de la forme suivante : Log(t)=-21og(D)+ (logK-21ogN) avec K=Kclog (a/Rcanne)By relying on the relation (1), it is possible for a given dimensioning and rotational speed to represent the sedimentation time of the particles as a function of their average diameter. We thus have the expression of a straight line in logarithmic scale of the following form: Log (t) = - 21og (D) + (logK-21ogN) with K = Kclog (a / Rcanne)
II est alors possible de définir le débit de gaz limite (Q) à la sortie de la centrifugeuse suivant l'expression suivante pour un volume de centrifuge donné (V) :It is then possible to define the limit gas flow rate (Q) at the outlet of the centrifuge according to the following expression for a given centrifugal volume (V):
Q=V/tQ = V / t
Au-delà des temps de sédimentation en fonction de la vitesse de rotation, il est utile de pouvoir estimer la surpression au paroi du à la force centrifuge appliquée. Au-delà de considérations touchant au calcul des éléments de structure, la surpression induite par la centrifugation doit favoriser le processus de condensation. En supposant un mouvement de base conduisant à une rotation de corps rigide et en négligeant l'influence des particules sur le gradient de pression, il est possible d'exprimer un profil de pression radial dans le centrifugeur par la relation suivante : Beyond the sedimentation times as a function of the rotational speed, it is useful to be able to estimate the pressure on the wall due to the centrifugal force applied. Beyond considerations relating to the calculation of structural elements, the pressure induced by centrifugation must favor the condensation process. Assuming a basic motion leading to a rigid body rotation and neglecting the influence of the particles on the pressure gradient, it is possible to express a radial pressure profile in the centrifuge by the following relation:
ouor
P (r) : pression local à la cote radiale r P (a) : pression local à la cote aP (r): local pressure at the radial dimension r P (a): local pressure at the dimension a
M : masse du gaz vecteurM: mass of the vector gas
T : température du milieuT: middle temperature
Ω : vitesse angulaire de rotationΩ: angular rotation speed
On peut ainsi en déduire des ordres de grandeurs de dimensionnement et de vitesse de rotation pour un flux à traiter donner.It is thus possible to deduce therefrom orders of sizing quantities and rotational speed for a flow to be treated.
La centrifugation est favorisée optionnellement par l'action combinée d'un champ électrostatique généré au sein de la zone de séparation, comme expliqué précédemment. La vitesse Uc de migration (ou de collecte) des particules de condensats par le seul effet électrostatique peut être exprimé par une relation du type :Centrifugation is optionally promoted by the combined action of an electrostatic field generated within the separation zone, as previously explained. The speed Uc of migration (or collection) of the condensate particles by the electrostatic effect alone can be expressed by a relation of the type:
Pour une nature (permittivité relative (εr) et un diamètre (D) ) de particules de condensât données, il est possible d'en déduire l'intensité (I) à appliquer à l'électrode de collecte pour obtenir une vitesse de migration donnée. Cet effet électrostatique s'additionne à l'effet de séparation inertielle dans la mesure où les particules sont électrisables dans des conditions standards de fonctionnement des électroprécipitateurs .For a nature (relative permittivity (ε r ) and a diameter (D)) of condensate particles given, it is possible to deduce the intensity (I) to be applied to the collection electrode to obtain a migration rate given. This electrostatic effect is added to the inertial separation effect since the particles are electrisable in standard operating conditions of electroprecipitators.
Il est à noter également qu'en appliquant une vitesse de rotation suffisante, une surpression locale au droit du média filtrant 54 induite par la force centrifuge favorise le phénomène de condensation.It should also be noted that, by applying a sufficient rotational speed, a local overpressure at the right of the filtering medium 54 induced by the centrifugal force favors the phenomenon of condensation.
Le média filtrant 54 permet de constituer une barrière d' impaction favorisant la recondensation des particules de contensat et l'enrichissement en condensats du côté de la calandre 7. Les éléments constitutifs du média sont avantageusement constitués d'éléments isolants thermiquement puis d'éléments conducteurs thermiques dans le sens radial allant de la zone interne du média filtrant 54 vers sa face externe (en regard avec la zone thermostatée 18) ; ceci pour assurer un maintien en température aussi bien du côté centrifugateur (l'intérieur de la virole 54) que du côté de la calandre 7 afin de favoriser le transfert du condensât puis son écoulement avant qu'il soit évacué par les systèmes de purge en continu 40.The filtering medium 54 makes it possible to constitute an impaction barrier favoring the recondensation of the contensate particles and the enrichment in condensates on the side of the shell 7. The constituent elements of the media advantageously consist of thermally insulating elements and then conductive elements. thermally in the radial direction from the inner zone of the filter media 54 to its outer face (facing the thermostated zone 18); this to ensure a temperature maintenance both on the centrifugal side (the inside of the shell 54) that the side of the shell 7 to promote the transfer of the condensate and its flow before it is discharged by the purge systems in continuous 40.
L'objectif est de former des agrégats de particules solides/liquides 69 sur les faces internes des plaques d' impactions 68 (figures 5 et 6) . Le léger gradient de température contrôlé et imposé par la zone thermostatée 18 permet alors une liquéfaction et la formation d'un film de condensât 98 (figure 7) évacuable par les jeux 69 aménagés entre les éléments d' impaction et de répartition de température 68 et le média (la virole 54) de séparation faisant également office de barrière thermique. Un jet de liquide de 71 frappe la calandre 7 et un film de liquide 73 se dépose sur celle-ci. Les passages 69 permettent par ailleurs de maîtriser la perte de charge au droit du média et de compenser son colmatage, notamment dans le cas où celui-ci est constitué d'éléments de captation par absorption-adsorption.The objective is to form aggregates of solid / liquid particles 69 on the inner faces of the impingement plates 68 (FIGS. 5 and 6). The slight temperature gradient controlled and imposed by the thermostated zone 18 then allows liquefaction and the formation of a condensate film 98 (FIG. 7) that can be evacuated by the clearances 69 arranged between the impaction and temperature distribution elements 68 and the media (the shroud 54) also serves as a thermal barrier. A liquid jet of 71 strikes the shell 7 and a film of liquid 73 is deposited on this one. The passages 69 also make it possible to control the pressure drop at the level of the media and to compensate for its clogging, particularly in the case where the latter consists of absorption-adsorption capture elements.
Les performances du dispositif de l'invention reposent sur les effets combinés de la centrifugation, de l'impaction, du refroidissement, du champ électrostatique, de la nucléation et enfin de la 1' adsorption. Néanmoins, au-delà de la combinaison de ces approches séparatives et de 1 ' adaptabilité du procédé, l'originalité de la présente invention réside dans la méthode de séparation/purification alliant un changement de phase et une séparation combinée. Pour parvenir à ce résultat et minimiser tout à la fois l'entraînement de gaz dans les condensats ou inversement, des condensats dans le flux gazeux, un film de matière solide constitué par les matières condensables (mélangées ou non à un média de condensation si l'objectif est de récupérer les condensables ou plutôt de valoriser le flux gazeux) constitue lui-même une interphase garantissant la séparation des flux. En effet, le flux de chaleur imposé sur la zone extérieure au média de filtration (zone thermostatée) permet de maintenir un équilibre et un gradient de température entre le film solide et les plaques d'impact et de répartition thermique. Ainsi, en passant progressivement d'un état solide à un état liquide, les condensables migrent à l'extérieur de la zone d'admission du gaz chargé de condensables vers la zone thermostatée tout en formant une pellicule évitant l'entraînement du gaz chargé. La conception de l'appareil permet par ailleurs de jouer sur l'épaisseur du film (en appliquant par exemple une température adaptée dans la zone thermostatée) pour obtenir des niveaux de performance séparatives plus ou moins importantes suivant la nature des condensables .The performance of the device of the invention is based on the combined effects of centrifugation, impaction, cooling, electrostatic field, nucleation and finally adsorption. Nevertheless, beyond the combination of these separative approaches and the adaptability of the process, the originality of the present invention lies in the separation / purification method combining a phase change and a combined separation. To achieve this result and to minimize both the entrainment of gas in condensates or vice versa, condensates in the gas stream, a film of solid material consisting of condensable materials (mixed or not with a condensing media if objective is to recover the condensables or rather to enhance the gas flow) is itself an interphase guaranteeing the separation of flows. Indeed, the heat flux imposed on the area outside the filtration media (thermostatically controlled zone) makes it possible to maintain an equilibrium and a temperature gradient between the solid film and the impact and thermal distribution plates. Thus, progressively passing from a solid state to a liquid state, the condensables migrate outside the inlet zone of the gas charged with condensables towards the thermostated zone while forming a film that avoids driving the charged gas. The design of the apparatus also makes it possible to play on the thickness of the film (for example by applying a suitable temperature in the thermostated zone) to obtain more or less important separative performance levels depending on the nature of the condensables.
Ce qui est expliqué précédemment pour la partie plaque de répartition est également applicableWhat is explained above for the distribution plate part is also applicable
(optionnellement) à la zone de média filtrant dans le cas où celle-ci est constituée de matériaux absorbants aptes à capter les espèces condensables. L'ajustement (en réglant par exemple la vitesse de rotation du dispositif ou en choisissant une nature de média d'absorption spécifique) entre force d'absorption et force centripète permet de contrôler le taux d'engorgement du média et par là même la quantité d'espèces condensables migrant vers la zone de collecte.(Optionally) the filter media zone in the case where it is made of absorbent materials capable of capturing the condensable species. The adjustment (for example by adjusting the rotational speed of the device or by choosing a type of specific absorption media) between the absorption force and the centripetal force makes it possible to control the clogging rate of the media and hence the quantity condensable species migrating to the collection area.
Suivant la nature des condensables (c'est- à-dire principalement selon leur comportement vis-à-vis de l'effet de condensation, de formation de solide ou de liquide plus ou moins visqueux) , il sera ainsi possible de privilégier l'une ou l'autre des adaptations technologiques séparatives précitées. On a représenté sur la figure 8 une vue en coupe d'un autre mode de réalisation d'un cryocondenseur pouvant être utilisé dans le cadre d'un dispositif d'épuration de flux gazeux conforme à l'invention. Il comporte un faisceau de tube 100 (deux tubes seulement ont été représentés sur la figure 8) à l'intérieur d'une virole cylindrique 102 elle-même fixée sur une bride 104. Les tubes 100 sont solidaires, à leurs extrémités supérieures, d'une bride 105, et à leurs extrémités inférieures, d'une bride 106. Une virole 108, réalisée par exemple en acier inoxydable, est montée sous la bride 106. Le gaz à épurer est introduit dans le faisceau des tubes 100, comme schématisé par les flèches 112. Il débouche dans le volume intérieur défini par la virole 108. Un liquide cryogénique par exemple l'azote liquide, circule autour des tubes 100 de manière à réaliser une trempe du gaz à épurer.Depending on the nature of the condensables (that is to say mainly according to their behavior vis-à-vis the effect of condensation, formation of solid or liquid more or less viscous), it will thus be possible to favor the one or other of the above-mentioned separative technological adaptations. FIG. 8 shows a sectional view of another embodiment of a cryocondensor that can be used in the context of a gas flow purification device according to the invention. It comprises a tube bundle 100 (only two tubes have been shown in FIG. 8) inside a cylindrical shell 102 itself. The tubes 100 are secured at their upper ends with a flange 105, and at their lower ends, with a flange 106. A ferrule 108, made for example of stainless steel, is mounted under the flange 106. The gas to be purified is introduced into the bundle of the tubes 100, as shown schematically by the arrows 112. It opens into the interior volume defined by the shell 108. A cryogenic liquid, for example liquid nitrogen, circulates around the tubes 100 so as to perform a quenching of the gas to be purified.
On a représenté sur la figure 9 un dévésiculeur à plaques utilisé en référence afin de comparer ses performances à celle d'un dispositif constitutif et conforme à l'invention (cryocondenseur) . Cet appareil de constitution simple, comporte un cône 120 à sa partie supérieure. Ce cône est raccordé à un cylindre extérieur 122 sur la paroi interne duquel sont disposées une série de plaques de formes coniques 124. Un tube intérieur 126 est disposé dans le tube 122 coaxialement à ce dernier. Le tube intérieur 126 porte lui aussi des plaques 128 coniques ou tronconiques . Le tube intérieur 122 et le tube extérieur 126 sont refroidis à une température de -50C à -1O0C par une circulation d'un fluide caloporteur généralement de l'eau glycolée. L'entrée de l'eau glycolée dans le tube extérieur a été représentée par la flèche 130 et sa sortie par la flèche 132. Les flèches 134 et 136 schématisent respectivement l'introduction et l'évacuation de l'eau glycolée dans le tube intérieur 126. Le flux à épurer est introduit à la partie supérieure du cône comme schématisé par la flèche 140. Il suit un parcours sinueux défini par les éléments tronconiques 124 et 128 avant de quitter l'appareil par sa partie inférieure comme schématisé par la flèche 142.FIG. 9 shows a plate separator used as a reference in order to compare its performance with that of a constituent device and in accordance with the invention (cryocondensor). This apparatus of simple constitution, has a cone 120 at its upper part. This cone is connected to an outer cylinder 122 on the inner wall of which are disposed a series of conical shaped plates 124. An inner tube 126 is disposed in the tube 122 coaxially with the latter. The inner tube 126 also carries plates 128 conical or frustoconical. The inner tube 122 and the outer tube 126 are cooled to a temperature of -5 0 C to -1O 0 C by a circulation of a coolant generally glycol water. The entry of the brine into the outer tube has been represented by the arrow 130 and its exit by the arrow 132. The arrows 134 and 136 schematize respectively the introduction and the evacuation of the brine in the inner tube. 126. The stream to be purified is introduced at the top of the cone as shown by the arrow 140. It follows a sinuous course defined by the frustoconical elements 124 and 128 before leaving the apparatus at its lower part as shown by the arrow 142.
Exemple : épuration de condensats de type goudronsExample: Purification of tar type condensates
Sans autres effets qu'une condensation des espèces condensables au moyen d'un dévésiculeur à plaques, le flux de gaz à traiter (gaz de pyrolyse de bio-masse réalisée aux environs de 5000C) comporte encore suffisamment de condensats pour perturber la mesure de débit donnée par un débitmètre de type Coriolis. La teneur en condensât dans le flux passe de 100gr/Nm3 à 10gr/Nm3 environ, (voir figure 10) .Without any effects other than a condensation of the condensable species by means of a plate separator, the flow of gas to be treated (pyrolysis gas of biomass produced around 500 0 C) still has enough condensates to disturb the measurement. flow rate given by a flow meter Coriolis type. The condensate content in the stream changes from 100 g / Nm 3 to 10 g / Nm 3 (see FIG. 10).
Les temps de passage des gaz à traiter sont de l'ordre de la dizaine de secondes. Dans le cas présent, deux dévésiculeurs à plaques disposés en série, par exemple du type représenté sur la figure 9, ont été utilisés pour obtenir le niveau d'épuration précité.The passage times of the gases to be treated are of the order of ten seconds. In the present case, two plate separators in series, for example of the type shown in FIG. 9, have been used to obtain the above-mentioned level of purification.
Pour améliorer l'épuration du flux gazeux vis-à-vis des goudrons, un dispositif cryocondenseur tel que celui représenté sur la figure 8 a été utilisé et implanté complémentairement à la suite des deux dévésiculeurs à plaques. Les essais d'épuration complémentaires avec ce dispositif (température de peau de -9O0C environ) ont permis d'observer la possibilité de former des particules de condensats de diamètres variables excédants rarement 0,5mm suivant l'humidité présente dans le gaz à épurer. Les temps de séjour dans cet appareil avoisinent la seconde.To improve the purification of the gaseous flow with respect to the tars, a cryocondensing device such as that represented in FIG. 8 was used and implanted complementarily following the two plate separators. The additional purification tests with this device (skin temperature of about -80 ° C.) made it possible to observe the possibility of forming condensate particles of variable diameters exceeding rarely 0.5 mm depending on the humidity. present in the gas to be purified. The residence times in this device are close to the second.
Le résultat de cette épuration a été représenté sur la figure 14. Les courbes des figures 10, 11 et 12 donnent des éléments chiffrés d'ordre de grandeur des paramètres de surpression locale au droit du média de séparation et les performances pouvant être attendues pour des diamètres de particules (vésicule et/ou solide) et des vitesses de rotation données.The result of this treatment is shown in FIG. 14. The curves of FIGS. 10, 11 and 12 give order-of-magnitude numerical elements of the local overpressure parameters at the separation media and the performances that can be expected for particle diameters (vesicle and / or solid) and given rotational speeds.
La figure 10 donne le rapport entre la pression locale et la pression à la paroi (P (r) /P (a) ) en fonction de la cote (r/a) . La figure 11 donne le temps de sédimentation en fonction du diamètre des particules (effet inertiel seul) et la figure 12 le débit maximal de gaz permettant d'atteindre le temps de sédimentation des particules. La figure 13 indique le débit mesuré par effet coriolis avec un séparateur à plaques et la figure 14 avec cryocondenseur et média filtrant.Figure 10 gives the relationship between the local pressure and the wall pressure (P (r) / P (a)) as a function of the dimension (r / a). Figure 11 gives the sedimentation time as a function of the particle diameter (inertial effect alone) and Figure 12 the maximum gas flow rate to reach the sedimentation time of the particles. Figure 13 shows the flow measured by coriolis effect with a plate separator and Figure 14 with cryocondenser and filter media.
Les calculs ont été réalisés avec les hypothèses suivantes :The calculations were made with the following assumptions:
A=O, ImA = O, Im
T=310K M=28g/molT = 310 K M = 28 g / mol
Rcanne=0, 01mRcanne = 0, 01m
Δp=984, 4kg/m3 η=l, 65.10"5Pa. sΔp = 984, 4 kg / m 3 η = 1.65 × 10 -5 Pa.s
V=O, 013m3 Nature des goudrons : naphtalène V = 0, 013m 3 Nature of tars: naphthalene

Claims

REVENDICATIONS
1. Dispositif d'épuration d'un flux gazeux contenant des vapeurs condensables, caractérisé en ce qu'il comprend une calandre (7) définissant un volume étanche, un refroidisseur (36) pour tremper le flux gazeux, un ensemble tournant (42) comprenant un rotor (44) et une virole cylindrique de séparation et filtration (54) montée sur le rotor et tournant avec lui, un tube support (48) monté sur le rotor (44) et portant un dispositif turbuleur-racleur (50), une électrode (94) entourant la virole de séparation et filtration (54) et une contre-électrode centrale (78) pour la création d'un champ électrostatique dans la calandre, une canne (78) de sortie du gaz épuré, une canalisation (40) de sortie des condensats assurant l'évacuation tout en garantissant l'étanchéité du système.1. Device for purifying a gas stream containing condensable vapors, characterized in that it comprises a shell (7) defining a sealed volume, a cooler (36) for quenching the gas stream, a rotating assembly (42) comprising a rotor (44) and a cylindrical separating and filtering sleeve (54) mounted on the rotor and rotating therewith, a support tube (48) mounted on the rotor (44) and carrying a scrubber-wiper device (50), an electrode (94) surrounding the separation and filtration ferrule (54) and a central counter-electrode (78) for the creation of an electrostatic field in the calandria, a purified gas outlet rod (78), a pipe ( 40) for condensate outlet ensuring the evacuation while ensuring the tightness of the system.
2. Dispositif d'épuration selon la revendication 1, caractérisé en ce que la virole de séparation et filtration (54) est constituée d'anneaux circulaires crénelés superposés (56) , une plaque d'impact et de séparation (64) étant fixée sur chacun des anneaux (56) de la virole.2. A purification device according to claim 1, characterized in that the separation and filtration ferrule (54) consists of superimposed crenellated circular rings (56), an impact and separation plate (64) being fixed on each of the rings (56) of the ferrule.
3. Dispositif d'épuration selon la revendication 2, caractérisé en ce que la virole de séparation et de filtration (54) est constituée d'anneaux thermiquement isolants et de plaques thermiquement conductrices pour assurer un transfert thermique maîtrisé entre la zone interne à la virole de séparation-filtration et une zone thermostatée (18) . 3. A purification device according to claim 2, characterized in that the separating and filtering ferrule (54) consists of thermally insulating rings and thermally conductive plates to ensure a controlled heat transfer between the inner zone to the ferrule. separation-filtration and a thermostatic zone (18).
4. Dispositif d'épuration selon la revendication 2 ou 3, caractérisé en ce que la virole de séparation et filtration (54) est constituée de matériaux absorbants aptes à capter les espèces condensables .4. A purification device according to claim 2 or 3, characterized in that the separation and filtration ferrule (54) consists of absorbent materials capable of capturing the condensable species.
5. Dispositif d'épuration selon l'une des revendications 1 à 4, caractérisé en ce que la zone thermostatée (18) entoure la virole de séparation et de filtration (54) . 5. A purification device according to one of claims 1 to 4, characterized in that the thermostatically controlled zone (18) surrounds the separating and filtering ferrule (54).
6. Dispositif d'épuration selon l'une des revendications 1 à 5, caractérisé en ce qu'il comporte une canne (78) de sortie du gaz épuré qui joue simultanément le rôle de contre-électrode. 6. A purification device according to one of claims 1 to 5, characterized in that it comprises a rod (78) of purified gas outlet which simultaneously acts as a counter-electrode.
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DE602005006021T2 (en) 2009-05-07
ATE391544T1 (en) 2008-04-15
US20080105127A1 (en) 2008-05-08
CA2591812A1 (en) 2006-07-06
DE602005006021D1 (en) 2008-05-21
WO2006070152A1 (en) 2006-07-06
ES2306281T3 (en) 2008-11-01
US7510599B2 (en) 2009-03-31
EP1833593B1 (en) 2008-04-09
JP2008525175A (en) 2008-07-17
CN101090763B (en) 2010-06-09
FR2879942A1 (en) 2006-06-30
FR2879942B1 (en) 2007-01-26
PL1833593T3 (en) 2008-09-30
ZA200704700B (en) 2008-09-25
CN101090763A (en) 2007-12-19
BRPI0519281A2 (en) 2009-01-06

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